Conversion of carbonaceous fuels into carbon free energy carriers

ABSTRACT

A system for converting fuel is provided and includes a first reactor comprising a plurality of ceramic composite particles, the ceramic composite particles comprising at least one metal oxide disposed on a support, wherein the first reactor is configured to reduce the at least one metal oxide with a fuel to produce a reduced metal or a reduced metal oxide; a second and reactor configured to oxidize at least a portion of the reduced metal or reduced metal oxide from the said first reactor to produce a metal oxide intermediate; a source of air; and a third reactor communicating with said source of air and configured to regenerate the at least one metal oxide from the remaining portion of the solids discharged from the said first reactor and the solids discharged from the said second reactor for by oxidizing the metal oxide intermediate.

CROSS-REFERENCE TO RELATED APPLICATION(S)

This is a continuation of U.S. patent application Ser. No. 14/504,295,filed on Oct. 1, 2014, now U.S. Pat. No. 9,376,318, which is adivisional of U.S. patent application Ser. No. 13/121,009, filed on Mar.25, 2011, now U.S. Pat. No. 8,877,147, which is a U.S. national stageentry of International Patent Application No. PCT/US2009/058579, filedon Sep. 28, 2009, which claims priority to U.S. Provisional PatentApplication No. 61/100,520, filed on Sep. 26, 2008, the entire contentsof all of which are fully incorporated herein by reference.

The present invention is generally directed to systems and methods ofconverting carbonaceous fuels. Reduction-Oxidation (redox) reactions,with the presence of one or more chemical intermediates, are generallyutilized to convert the carbonaceous fuels.

In order to meet the ever increasing demand for clean and affordableenergy carriers and to ensure the sustainable growth of modern economy,efficient and environmentally friendly technologies that convertcarbonaceous fuels such as coal, crude oil, natural gas, biomass, tarsands, and oil shale into carbon free energy carriers are highlydesirable. An energy carrier is a substance or phenomenon that can beused to produce mechanical work or heat or to operate chemical orphysical processes.

Existing carbonaceous fuel conversion technologies are either capitalintensive (gasification or ultra-supercritical pulverized coalcombustion), have low efficiencies (sub-critical pulverized coalcombustion), or both, especially when CO₂ regulation is mandatory.

Chemical reactions between carbonaceous fuels and air/steam/CO₂ throughthe assistance of a metal oxide medium may represent an effective way toconvert the fuels. A number of techniques have been proposed to convertcarbonaceous fuels using metal oxide. For example, Watkins, U.S. Pat.No. 3,027,238, describes a method for producing hydrogen gas includingreducing a metal oxide in a reducing zone, and oxidizing the reducedmetal with steam to produce hydrogen in an oxidizing zone. Thomas etal., U.S. Published Application No. 2005/0175533, and Fan et al., PCTApplication No. WO 2007/082089, both describe methods for producinghydrogen gas by reducing a metal oxide in a reduction reaction between acarbon-based fuel and a metal oxide to provide a reduced metal or metaloxide having a lower oxidation state, and oxidizing the reduced metal ormetal oxide to produce hydrogen and a metal oxide having a higheroxidation state. The metal or metal oxide is provided in the form of aporous composite of a ceramic material containing the metal or metaloxide.

A well known process is a steam-iron process wherein coal-derivedproducer gas is reacted with iron oxide particles to be laterregenerated with steam to produce hydrogen gas. However, a fluidized bedis used in this system which causes iron (Fe) to loop between FeO andFe₃O₄, the gas is not fully converted, and no pure gas stream can beproduced. Ishida et al., U.S. Pat. No. 5,447,024, describes processesthat make use of nickel oxide particles to convert natural gas through achemical looping process into heat to be used in a turbine. However,this technology has limited applicability because it can only convertcostly natural gas into heat/electricity. Therefore, both the feedstockand the product of the process are restricted.

With increasing demand for cleaner and more efficient energy carrierssuch as electricity, hydrogen, and fuels, the need arises for improvedsystems, and system components therein, which produce the aforementionedenergy carriers with higher efficiency and lower emissions.

Embodiments of the present invention provide novel systems and processesfor converting solid, liquid, and gaseous fuels into efficient energycarriers. In one embodiment, a system for converting solid, liquid, orgaseous fuel is provided and comprises a first reactor comprising aplurality of ceramic composite particles. The ceramic compositeparticles comprise at least one metal oxide disposed on a support, andthe first reactor is configured to reduce the at least one metal oxidewith a fuel to produce a reduced metal or a reduced metal oxide. Thesystem includes a second reactor configured to at least partiallyre-oxidize the reduced metal or reduced metal oxide to produce a metaloxide intermediate. The system also includes a source of air and a thirdreactor communicating with the source of air and configured toregenerate the at least one metal oxide by oxidizing the metal oxideintermediate. In a preferred form, the fuel is a solid fuel or a gaseousfuel. Optionally, a fuel conversion enhancement gas, preferablyincluding CO₂, steam, and/or H₂, is sent to the first reactor in whichthe gas flows countercurrently to the flow of solids.

Also provided is a method of preparing ceramic composite particles, forexample in the form of pellets, comprising the steps of, mixing a metaloxide with at least one ceramic material to form a mixture, granulatingthe mixture, and drying the granulated mixture. The dried, granulatedmixture is processed into particle form such that the characteristiclength of the particles is greater than about 200 μm. The particles areheat treated at a temperature of from about 500 to about 1500° C. andoptionally may be reduced and oxidized prior to use in the reactorsystem.

Additional features and advantages provided by embodiments of thesubject matter described herein will be more fully understood in view ofthe following detailed description, the accompanying drawings, and theappended claims.

The following detailed description of the illustrative embodiments ofthe subject matter described herein can be best understood when read inconjunction with the following drawings, where like structure isindicated with like reference numerals and in which:

FIG. 1 is a schematic illustration of one embodiment in which a systemfor producing hydrogen and/or electricity from coal and/or biomasswithout the need for an Air Separation Unit (ASU) is provided;

FIG. 2A is a schematic illustration of a reducer that converts coaland/or biomass into CO₂ and steam, while reducing Fe₂O₃ in the compositeparticles into Fe and FeO; FIGS. 2B and 2C illustrate an alternativedesign for solid fuel injection and reactor outlet ports in the reducer;

FIG. 3 is a schematic illustration of a coal char/biomass conversionenhancement scheme;

FIGS. 4A and 4B are schematic illustrations of gas solid flow patternsin the first and second stages of a reducer;

FIG. 5 is a chart showing the conversion of coal and an oxygen carrierin an embodiment of a moving bed reducer;

FIG. 6 is a schematic illustration of an alternative embodiment for asystem that converts carbonaceous fuels into hydrogen, sequestrable CO₂,and heat;

FIG. 7 illustrates a heat integration scheme for an embodiment of acarbonaceous fuel conversion system;

FIG. 8 is a schematic illustration of a system that converts gaseousfuels such as syngas, methane, and other hydrocarbons, into hydrogenand/or electricity;

FIG. 9 is a chart showing the conversion of syngas and iron oxide in amoving bed reducer;

FIG. 10 is a chart showing the conversion of methane and iron oxide in amoving bed reducer;

FIG. 11 is a chart showing the concentration of hydrogen produced from amoving bed oxidizer;

FIG. 12 is a chart showing the crushing strength of an Fe₂O₃-based metaloxide composite particle made in accordance with an embodiment of thepresent invention;

FIG. 13 is a chart showing the attrition rate of oxygen carrierparticles after a number of redox cycles;

FIG. 14 is a chart showing the reduction-oxidation rates of the oxygencarrier particles with respect to number of redox cycles;

FIG. 15 is a chart showing the reactivity of the oxygen carrier particleafter reacting with coal for four reduction-oxidation cycles, syngas forthree reduction-oxidation cycles, and natural gas for onereduction-oxidation cycle;

FIG. 16 is a graph illustrating the desired operating line of oneembodiment of the reducer.

FIG. 17 is a schematic illustration of an embodiment for electricitygeneration from biomass;

FIG. 18 is a schematic illustration of an embodiment forhydrogen/electricity generation from natural gas or other methane richgas;

FIG. 19 is a schematic illustration of a design for the redox systemusing non-mechanical gas seals and solids flow control device; and

FIGS. 20A-D illustrate alternative designs for non-mechanical gassealing and solids flow control.

Referring generally to FIGS. 1 and 8, embodiments of the subject matterdescribed herein are directed to systems and methods for convertingcarbonaceous fuels by the redox reaction of metal oxide ceramiccomposites into carbon-free energy carriers such as hydrogen, heat, andelectricity. FIG. 1 illustrates one embodiment of a system configurationwhen solid carbonaceous fuels are used directly as the feedstock, whileFIG. 8 illustrates one embodiment of a system configuration when gaseouscarbonaceous fuels are used as the feedstock.

In the embodiment illustrated in FIG. 1, system 10 includes a firstreactor 12, also termed the reducer herein, which is configured tooxidize solid carbonaceous fuel from fuel source 14 into CO₂ and steamwhile reducing the metal oxide based ceramic composite particles whichact as the oxygen carrier in the system. The solid fuel may be suppliedby entraining it a flow of gas such as an oxygen-containing gas. Asshown, a supply of metal oxide composite particles is stored in vessel16 and supplied to reducer 12 as needed. Additional composite particlesmay be added as needed via conduit 11 as shown in FIG. 1. The heatrequired or generated in reducer 12 is provided or removed, at leastpartially, by the metal oxide oxygen carrier particles. The combustionproducts of the fuel, CO₂ and steam, are removed from reducer 12 throughline 18. As shown, the steam is condensed by passing the gaseous streamthrough a heat exchanger 19 which is fed with a coolant such as waterfrom line 21. The CO₂ stream , after optional removal of contaminantssuch as mercury in separator 20, is sent for sequestration. Typically, arelatively pure (i.e., >95%) CO₂ stream is produced from the reducer 12.

The second reactor 22, also termed the oxidizer herein, is configured to(partially) oxidize a portion or all of the reduced metal oxide oxygencarrier particles with either steam and/or CO₂ and to produce a streamof substantially pure hydrogen. The hydrogen is removed from oxidizer 22through line 23. As shown, the hot hydrogen stream may be used to heatincoming steam in line 40 using heat exchanger 25. Any contaminants,such a hydrogen sulfide gas, in the hydrogen stream may be removedthrough separator 27. The hydrogen gas may be used, for example, forelectric power generation, liquid fuel synthesis, or other uses. Thethird reactor 24, also termed the combustor herein, combusts thepartially oxidized metal oxide oxygen carrier particles from oxidizer 22and the remaining reduced metal oxide oxygen carrier particles fromreducer 12 using an oxygen containing gas such as air supplied, forexample, via line 26 through optional compressor 28. In the case whenreducer 12 requires additional heat, at least part of the heat generatedfrom combustor 24 is integrated to the reducer. In some cases, an airseparation unit (not shown) can be used to separate oxygen from air andsend the oxygen into the reducer to partially combust the fuel and toprovide additional heat to the reducer 12. However, the capacity of suchan air separation unit is much smaller than that used in a conventionalgasification plant with identical fuel processing capacity. Therefore,one advantage of the system and process illustrated in FIG. 1 is that itcan reduce the size of the air separation unit or eliminate the need forthe air separation unit which separates oxygen from air. This reducesthe capital cost of building and operating the fuel conversion systemand enhances the overall efficiency of the system. In preferredembodiments, the air separation unit is completely avoided. Although thesystem illustrated in FIG. 1 depicts solid fuel conversion, gaseous fueland liquid fuel can also be converted using this system. The operatingpressure in the combustor 24 can either be comparable to the pressuresin the reducer and oxidizer, or may be different. In the former case,non-mechanical based solids and gas flow control devices can beconveniently used to connect the reactors. In the latter case,mechanical valves should be used. However, the combustor can be operatedat lower pressures, resulting in reduced combustor energy consumption.Moreover, heat can be extracted from the solids discharged from thereducer so that the oxidizer is operated at temperatures significantlylower than those of the reducer. By doing this, the steam to hydrogenconversion is enhanced.

As shown in FIG. 1, hot spent air from combustor 24 can be optionallysent to an expander 60 coupled to a turbine 62 and a generator 64 andused to generate electricity 66. Exhaust gas from the expander may besent to separation equipment for the removal of contaminants such assulfur oxides and nitrogen oxides.

Additional heat can be produced by means of: i) introducing a smallerfraction of the reduced metal oxide oxygen carrier particles fromreducer 12 into oxidizer 14, with the remaining reduced metal oxideoxygen carrier particles being directly introduced to combustor 24; orii) introducing a sub-stoichiometric amount of steam and/or CO₂ tooxidizer 22 so that the reduced metal oxide oxygen carrier particles areincompletely regenerated by the steam and/or CO₂.

The oxygen carrier comprises a plurality of ceramic composite particleshaving at least one metal oxide disposed on a ceramic support. Suitableceramic composite particles for use in the system and process of theinvention are described in Thomas U.S. Published Application No.2005/0175533, and Fan et al., PCT Application No. WO 2007/082089. Inaddition to the particles and particle formula and synthesis methodsdescribed in Thomas, in a further embodiment described below, methods toimprove the performance and strength of the ceramic composite particleshave been developed.

The further embodiment includes the step of mixing a metal oxide with atleast one ceramic support material in powder form followed by anoptional granulation step with the addition of either water or a bindingmaterial such as starch, sodium silicate, and/or potassium silicate. Apromoter material may be added in the mixing step before granulation.The granulated powder is then dried at temperatures of between about50°-500° C. in air or nitrogen to reduce the moisture content to below10%. The granulated powder is then processed into pellets with acharacteristic length larger than about 200 μm. The methods forconverting granulated powders into pellets may include, but are notlimited to, extrusion, granulation, and pressurization methods such aspelletization. The pressure used to produce the pellets ranges fromabout 0.1-25 MPa.

After the metal oxide containing ceramic composite particles are made,final treatment steps are carried out. The final treatment steps includesintering the particles at 500°-150020 C., followed by reducing themetal oxide in the particles with hydrogen and then oxidizing theparticles with air for at least one reduction-oxidation cycle tostabilize the performance of the particles. It should be noted thatspent powders resulting from attrition in the reactor system can bereprocessed and reactivated following this method.

The metal oxide component preferably comprises a metal selected from thegroup consisting of Fe, Cu, Ni, Sn, Co, Mn, In, and combinationsthereof. The support material comprises at least one component selectedfrom the group consisting of SiC, oxides of Al, Zr, Ti, Y, Si, La, Sr,Ba, and combinations thereof. These supports include naturally ores suchas bentonite and sepiolite. The ceramic composite comprises at leastabout 10% by weight of the support material. In further embodiments, theparticle comprises a promoter material. The promoter comprises a puremetal, a metal oxide, a metal sulfide, or combinations thereof. Thesemetal based compounds comprise one or more elements from the groupconsisting of Li, Na, K, Rb, Cs, Be, Mg, Ca, Sr, Ba, B, P, V, Cr, Mn,Co, Cu, Zn, Ga, Mo, Rh, Pt, Pd, Ag, and Ru. The ceramic compositecomprises up to about 20% by weight of the promoter material. In anexemplary embodiment of the ceramic composite, the metal oxide comprisesFe₂O₃ supported on a support which is a mixture of alumina (Al₂O₃) andAnatase (TiO₂).

Referring back to the reduction reaction taking place in reducer 12, thereducer utilizes solid carbonaceous fuel such as coal, tars, biomass,oil shale, oil sands, tar sand, wax, coke, and the like to reduce theleast one metal oxide of the ceramic composite particles to produce amixture of reduced metal and/or metal oxide. The fuel is preferablysupplied in particulate form to the reducer. The possible reductionreactions include but not limit to:

2Fe₂O₃+C→4FeO+CO₂

C+CO₂→2CO

C+H₂O→CO+H₂

Fe₂O₃+CO/H₂→2FeO+CO_(2/)H₂O

FeO+CO/H₂→Fe+CO_(2/)H₂O

Preferred designs of the reducer include a moving bed reactor with oneor more stages, a multistage fluidized bed reactor, a step reactor, arotary kiln, or any other suitable reactor or vessel known to thoseskilled in the art. In any of the reactor designs, a counter-currentflow pattern between the metal oxide oxygen carrier solid particles andthe gas is used to enhance the gas and solid conversion. Thecounter-current flow pattern minimizes the back-mixing of both the metaloxide composite oxygen carrier solids and gas. Moreover, thecounter-current flow maintains the solids outlet 28 of the reducer 12 ina more reductive environment, while the gas outlet 30 of reducer 12 ismaintained in a more oxidative environment. As a result, the gas andsolid conversion are both enhanced based on thermodynamic principles.

FIG. 16 exemplifies a preferred operating line of a reducer using syngasas the feedstock based on thermodynamic analysis. The preferredoperating line (solid straight line) corresponds to full conversion(>99% conversion) of gaseous syngas fuel into CO₂ and steam whilereducing the oxygen carrier particles, such as iron oxide containingcomposite particles, by nearly 50%. Similarly, a preferred operatingmode when a solid fuel such as coal is used will lead to full conversion(>99% conversion) of coal into CO₂ and steam while reducing the ironoxide oxygen carrier composite particles by 33-85% depending on theranking of the coal. Generally speaking, the operating conditions in thereducer are configured so that at least 95% of the carbonaceous fuel isconverted to a gas stream with high CO₂ and steam concentration whilereducing the iron oxide in the composite particles by 33% -85%. Thepreferred iron oxide reduction rate is about 36-85%. Preferably, thereduced iron oxide should have a metallic iron to Wuestite molar ratioof between about 1:25 to 3.55:1.

The conversion of carbonaceous fuel is defined as:

X _(gas) =n _(o) _(_) _(consumed) /n _(o) _(_) _(fullconversion)

n_(o) _(_) _(consumed) refers to number of moles of oxygen transferredto the fuel from the oxygen carrier in the reducer; n_(o) _(_)_(fullconversion) represents number of moles of oxygen required toconvert the fuel fully into CO₂ and steam.

The conversion of iron oxide (or any type of metal oxide describedabove) is defined as:

$y = {\frac{{{\hat{n}}_{O}/{\hat{n}}_{Fe}} - {n_{O}/n_{Fe}}}{n_{O}/n_{Fe}} \times 100\%}$

Here, n_(O)/n_(Fe) corresponds to the molar ratio between the oxygen andiron atoms in Fe₂O₃, while {circumflex over (n)}_(O)/{circumflex over(n)}_(Fe) corresponds to the molar ratio between the oxygen and ironatoms in the reduced solid product, i.e. FeO_(x) (0<×<1.5). For example,the reduction of Fe₂O₃ to Fe₃O₄ corresponds to a solid conversion of(3/2-4/3)/(3/2)×100% =11.11%, FeO corresponds to a conversion of 33.33%,and Fe corresponds to 100% solid conversion. Definition of theconversion of other metal oxides follows a similar definition. A similardefinition applies when other metals are used.

FIG. 2 illustrates a specific embodiment of a reducer 12 configured forsolid carbonaceous fuel conversion. A two stage moving bed is provided.The upper stage 32 (first stage) converts the gaseous phase from thelower stage 34 (second stage) and volatiles from the solid fuel into CO₂and steam, while the lower stage 34 converts the solid fuel such aspulverized (i.e., particulate) coal, coke biomass, or coal char which isfed into the reducer from line 14. The metal oxide particles which enterthe first stage through line 70 as, for example, Fe₂O₃-containingparticles, exit the second stage as a mixture of reduced metal (e.g.,Fe) and metal oxide (e.g., FeO) through line 28 . An oxygen-containinggas and, optionally a combustion enhancing gas such as CO₂, H₂O, or H₂,is fed into the bottom of the second stage through line 74; the hotcombustion gases, CO₂ and steam, exit the top of the first stage throughline 18. For example, when Fe₂O₃-containing particles are used as theoxygen carrier, the Fe₂O₃ conversion is between 20% -85%. The two stagedesign of the reducer allows good mixing of both solid-solid andsolid-gas. Moreover, the solids movement can be achieved with ease. Incertain embodiments, a portion of the pulverized solid fuel is entrainedby the gaseous phase in the reducer. As a result, a portion of the solidfuel moves upwardly and is combusted in both the first and secondstages. Thus, the height of the second reactor stage can either besignificantly shorter or longer than the height of the first reactorstage depending on the physical and chemical properties of the fuel andthe operating conditions in the reactor. Because of the flexibility inthe reactor design, the point of injection of the solid fuel may bevaried to any position between the reducer inlet and the reducer outlet.

In certain embodiments, pulverized solid fuel, which is injected throughline 14 into the reducer between the first and second reducer stages 32and 34, is entrained by the gaseous phase in the reducer and flowscounter-currently against the metal oxide oxygen carrier particulatesolids. The solid fuels are converted to CO₂ and steam during theentrainment step. At least 95% of the fuel will be converted beforeexiting from the top of the first stage of the reducer 12. A portion ofthe ash can also be entrained and removed from the top of the firststage of the reducer. As shown in FIGS. 2B and 2C, the pulverized solidfuel may be injected into the reactor at multiple locations to betterdistribute the fuel in the reactor.

The reactions that take place in the first and second stages of reducer12 include:

Particle reduction: CH₄+4Fe₂O₃→CO₂+2H₂O+8 FeO

Coal devolatilization: coal→C+CH₄

CO+FeO→Fe+CO₂

C+CO₂→2O

Char gasification and particle reduction:

C+CO₂→2CO

C+H₂O→CO+H₂

CO+FeO→Fe+CO₂

H₂+FeO→Fe+H₂O

One of the issues related to conversion of solid fuel is the enhancementof solid fuel conversion. FIG. 3 illustrates a scheme to enhance thesolid conversion by adding CO₂ to the bottom of the second reducer stagein FIG. 2. The addition of CO₂ initiates a “chain reaction” thatgasifies carbon while reducing metal oxide. During this process, moreCO₂, which acts as gasification enhancer, will be produced, resulting infurther improved reaction rates. Other gasification enhancers includeH₂O and H₂. It should be noted that although injection of CO₂ and H₂Omay affect slightly the metal oxide conversion, they are stillconsidered as feasible gasification enhancers since they are easilyavailable in the fuel conversion system. One way to obtain suchenhancers is to recycle part of the exhaust gas from the first stage ofthe reducer, which contains both CO₂ and steam, into the second reducerstage solids outlet (bottom). The aforementioned fuel conversionenhancement technique can also be applied for the conversion ofgaseous/liquid carbonaceous fuels such as methane and higherhydrocarbons since CO and H₂ react with metal oxide faster thanhydrocarbon or solid fuels.

FIG. 4 further illustrates a preferred design of the solids outlet(bottom) of the first stage of the reducer as well as the solids outlet(bottom) of the second stage of the reducer. The first stage has arestricted flow outlet such as, for example, a funnel shaped outlet 36with multiple blades 38 on the interior wall. Such a design allows gasto permeate from the top of the second stage to the first stage.Meanwhile, the metal oxide based ceramic composite particles will bedischarged from outlet 36 in a controlled manner. A dune of solidparticles is formed between the bottom of the first stage and the top ofthe second stage. Solid fuel is dispersed to the annular region 40 ofthe first stage and mixes well with the metal oxide based ceramiccomposite particles. The solids outlet 42 of the second stage also usesa restricted flow design such as a funnel shape. The funnel preferablyhas an angle of about 15-75°. Such an angle allows solids with differentsizes to move downwardly at similar speeds, thereby avoiding smallsolids exiting the reducer at rates much faster than the larger solids.Moreover, the solids will act as a gas distributor to ensure good mixingbetween solid and gas. In certain embodiments, multiple funnel shapedsolids outlets can be used, especially for the first stage outlet. FIG.2, especially FIGS. 2B and 2C, illustrates one example of an outletdesign in which three funnel shaped outlets 36 a, 36 b, and 36 c areused with three solid fuel injection ports 14 a, 14 b, and 14 c. Thisdesign provides a more homogenous solids distribution in the reactor.Other configurations of funnel shaped outlets and solid fuel injectionports can also be used.

The effective regulation of gas and solids flows between the reactors isimportant. Mechanical valves such as rotary valve or a ball valve-tablefeeder system can be used to control the solids and gas movements.Non-mechanical valves, loop seals, and/or zone seals can also be used toregulate the gas and solids flow. Several suitable non-mechanical gassealing and solids flow control devices are schematically illustrated inFIGS. 20A-D. These devices can be installed between reactors or reactorstages to control the flow of materials between stages.

FIG. 5 further illustrates in chart form the conversion of an iron oxidebased particulate oxygen carrier and coal obtained in a moving bedreducer. More detailed results are listed in Table 1 below.

TABLE 1 Summary of the Fuel Reactor demonstration results using coal,coal char, and volatile Coal Lignite Bituminous Anthracite Type of FuelVolatile Char Char Coal Fuel Conversion (%) 99.8 94.9-99.5 90.5 95.5 CO₂Concentration in 98.8 99.23 99.8 97.3 Exhaust (% Dry Basis) GasificationEnhancer H₂/CO₂ CO₂/H₂O CO₂ CO₂Generally speaking, solid fuel conversion of >90% with about 33%-85%metal oxide conversion can be obtained. The exhaust gas stream from thereducer has >95% CO₂ after condensing out steam.

Referring now to FIG. 17, where like reference numerals represent likeelements, an embodiment for electricity generation from biomass is shownin schematic form. The configuration is similar to that shown in FIG. 1.In this embodiment, all of the reduced metal oxide particles aredirectly sent to the combustor 24. As a result, the oxidizer (not shown)is completely bypassed. A preferred configuration for the reducer ofthis embodiment is shown in FIG. 2. The hot gas stream generated fromthe system can be either used in a boiler/Heat Recovery Steam Generator(HRSG) or in a combined cycle system with an expander/gas turbine forpower generation. Similarly, the combustor hot gas in the embodimentshown in FIG. 1 can also be used in a boiler/HRSG, although an expanderis shown in FIG. 1 for illustrative purposes. The metals that can beused in the process shown in FIG. 1 include Fe, Ni, Cu, and Mn. WhenFe₂O₃ is used, the preferred solid reduction rate is 11%- 75% for powergeneration purposes. Table 2 shows the experimental result obtained frombiomass gasification:

TABLE 2 Experimental results obtained from pulverized woody biomassusing Fe₂O₃ based ceramic composite and gasification enhancer (CO₂ andH₂O) CO₂ Concentration Metal in the Biomass Residence Oxide ReducerExhaust Conversion Time Reduction (% dry basis) (%) (Min) (%) >95% >99%20-120 >20%

In some cases the solid fuel may contain impurities such as ash, sulfur,and mercury. Ash in the solid fuel will exit the reducer along with themetal oxide based ceramic composite. Part of the sulfur will also exitthe reducer in the form of metal-sulfur compounds such as FeS(Fe_(0.877)S) at high temperatures. The remainder of the sulfur exitsthe reducer in the form of H₂S/SO₂. The sulfur can be sequestrated alongwith CO₂ without the need for treatment. All the mercury will also exitthe reducer along with exhaust gas stream. The mercury can either beremoved using known techniques or be sequestered.

Referring back to FIG. 1, a portion of the solids exiting reducer 12will enter second reactor 22 (the oxidizer). Preferred designs of theoxidizer include a moving bed reactor, a multistage fluidized bedreactor, a step reactor, a rotary kiln, or any other suitable reactor orvessel known to those skilled in the art. In any of the reactor designs,a counter-current flow pattern between oxygen carrier solid particlesand gas is used to enhance the gas and solid conversion. Thecounter-current flow pattern minimizes the back-mixing of both oxygencarrier solid and gas. Moreover, the counter-current flow keeps thesolids outlet of reactor 22 in a more oxidative environment while thegas outlet of reactor 22 is maintained in a more reductive environment.As a result, the gas and solid conversion are both enhanced.

The connections between the reducer 12, oxidizer 22, and combustor 24can be mechanical, i.e. a rotary valve or a lock hopper assembly. Inanother design, the reducer 12, oxidizer 22, and combustor 24 aredirectly connected using non-mechanical valves and gas seals such asthose used in a circulating fluidized bed or a fluid catalytic cracker.The pressure differences in the reactor as well as a small amount ofaeration gas prevent the leakage of the product gas from the oxidizer 22into the reducer 12 or vice versa. Such a non-mechanical reactor designis illustrated in FIG. 19. Only one of the three connections (“A”, “B”,and “C” in FIG. 19) is used to control the overall solids circulationrate in the reactor system. Preferably, the connection between theoxidizer 22 and the combustor 24 (connection “C” in FIG. 19) is used toregulate the solids flow. Suitable non-mechanical valves for thisconnection between reactor stages include L-valves, J-valves, loopseals, or

N-valves. Aeration gas used here can be steam and/or spent air. For theconnection between the combustor 24 and reducer 12 (connection “A” inFIG. 19), a zone seal or loop seal can be used with CO₂ and/or spent airas the aeration gas. For the connection between the reducer 12 andoxidizer 22 (connection “B” in FIG. 19), a zone seal or loop seal can beused with H₂ and/or steam as the aeration gas. Preferred designs for thenon-mechanical gas seal and solids valves are shown in FIG. 20A(N-valve), FIG. 20B (L-valve), FIG. 20C (loop seal), and FIG. 20D(standpipe and zone seal). Relatively smooth, funnel shaped reactoroutlets are installed for both the reducer 12 and oxidizer 22 to ensurea smooth connection between the reactor (with large inner diameter) andthe non-mechanical devices (with much smaller inner diameters). Thisreduces the usage of aeration gases. A particulate separation device(not shown) may also installed between the combustor 24 and reducer 12.The device is used to separate out the fines from the combustor exhaustgas. A preferred separation device has more than a two stages. The firststage separates out larger particulates (e.g., 20−200+ 82 m) from thefine powder and exhaust gas. The second stage separates out smallerfines from the exhaust gas. The fines may be reprocessed into largerparticles/pellets.

The gaseous feedstock for oxidizer 22 can either be steam, CO₂, or acombination thereof and enters through line 40. When steam is used, thesteam conversion of the oxidizer can be between about 50-99% dependingon the oxidizer temperature and solid conversion in the reducer. WhenFe₂O₃ based ceramic composite particles are used, an iron phase of atleast 5% (by mole) is preferred in order to achieve optimum steamconversion. When CO₂ is used, the gas conversion (40-95%) is alsodependant upon the temperature and solid conversion. When a mixture ofCO₂ and steam is used, the oxidizer product stream can be condensed andpartially recycled to reduce the CO₂ concentration in the final productstream and to improve the gas conversion.

The metal-sulfur compounds formed in reducer 12 will be partiallyregenerated in oxidizer 22, producing H₂S. Therefore, the product streamof the oxidizer is often contaminated with H₂S up to 750 ppm. H₂S can beremoved via sorbent techniques, solvent techniques, or other traditionalacid removal techniques. The ash in the metal oxide ceramic compositewill not react in the oxidizer and will be discharged along with thepartially regenerated metal oxide ceramic composite. When Fe₂O₃ basedceramic composite is used, the iron phase in the solid product from theoxidizer is predominantly Fe₃O₄ with some remaining metal-sulfurcompounds. In certain embodiments, a sub-stoichiometric amount ofsteam/CO₂ is introduced to regenerate the reduced iron oxide to anoxidation state lower than Fe₃O₄, e.g. Fe/FeO mixture, FeO, or FeO/Fe₃O₄mixture. By doing this, the heat that can be generated from thesubsequent combustor will increase at the expense of reduced hydrogen/COproduction in the oxidizer.

Referring back to FIG. 1, the partially regenerated metal oxide ceramiccomposite particles from the oxidizer are introduced to the thirdreactor 24 (the combustor) along with a portion of the reduced ceramiccomposite particles from the reducer 12. Preferred designs of thecombustor 24 include a fast fluidized bed reactor, an entrained bedreactor, a transport bed reactor, or a mechanical conveying system.Optionally, to provide sufficient time for metal oxide ceramic compositeregeneration, a two stage design may be adopted for the third reactor24. With such a design, stage I of the third reactor, which is locatedat the bottom portion, is operated in a bubbling or turbulentfluidization regime to provide adequate solids and gas residence time.The diameter of stage I is typically larger than stage II when such adesign is used.

The combustor 24 is used to substantially completely oxidize the metaloxide based ceramic composite back to its higher oxidation state. Air orother oxygen containing gas may be used in the combustor. The gaseousproduct from the combustor is an oxygen lean gas at a temperature muchhigher than the inlet gas temperature. The gaseous product may alsocontain SO₂ and NO_(x). When Fe₂O₃ based ceramic composite is used, theiron phase in the solid product is predominantly Fe₂O₃. Ash will alsocome out along with the fine ceramic composite powders resulting fromattrition. A portion of the ash may exit from the gaseous outlet of thereducer.

A significant amount of heat is generated in the combustor 24. In oneconfiguration, the heat is carried away from the combustor by both thegaseous product and solid product. The solid product is directlyinjected back to the reducer 12 through line 42. As a result, thesensible heat carried in the solid product is used to compensate theheat required in the reducer 12. Moreover, the sensible heat containedin the exhaust gas can also be transferred to the reducer via heatexchange.

Ash and spent ceramic composite can be separated using mechanicalmethods such as a cyclone. Ash separation efficiency was demonstrated tobe at least 75.8% with 15 seconds of mechanical separation, whichcorresponds to less than 1% ash content in the ceramic composite whenbituminous coal is used as the solid fuel.

Before Experiment Pellet (g) Ash (g) 2565.3 224.97681 After ExperimentPellet (>2.8 mm) Particle (<2.8 mm) Pellet (g) Ash (g) Particle (g) Ash(g) 2444.2 54.4 121.1 170.5

Referring now to FIG. 6, FIG. 6 exemplifies an alternative configurationfor a fuel conversion system. In this configuration, where likereference numerals represent like elements, the first reactor 12integrates the function of both the reducer and the combustor (such asshown in the configuration in FIG. 1). The first reactor 12 has a shellside 13 and a tube side 15. Solid or gaseous carbonaceous fuel isintroduced into shell side 13 through line 14, and ceramic compositeparticles, supplied from vessel 16, are converted (i.e., reduced) in theshell side as well. A portion of the reduced solids from the shell sideis directly recycled back to the tube side through conduits 19 andcombusted with air. The heat released in the combustion compensates forthe heat required in the shell side. Moreover, the hot solids from thethird reactor 24 (combustor) will also partially compensate for the heatrequired in the reducer 12. Steam and CO2 are supplied to oxidizer 22through port 40, while the hydrogen stream is removed through line 23.Ceramic composite particles with regenerated metal oxide are sent fromcombustor 24 back to vessel 16. The heat from those particles may becaptured and used for steam or power generation (indicated by line 35.ash and spent particles are removed via line 37.

Referring now to FIG. 7, where like reference numerals indicate likeelements, FIG. 7 illustrates a generalized heat integration scheme forthe process. In such a scheme, heat generated in the combustor 24 isused to: 1) compensate for the heat requirements in the reducer 12, and2) generate electricity for parasitic energy consumption. The goal ofthe heat integration is to minimize the excessive heat generated in thesystem, thereby maximizing the energy conversion from the fuel to theproduct. As shown, the metal oxide particles are reduced in reducer 12,with reduced particles sent via lines 94 and 96 to the oxidizer 22 andcombustor 24. Oxidized particles 98 are sent from oxidizer 22 tocombustor 24, while regenerated particles 92 are recycled back toreducer 12. The heat produced by the reactions, shown as arrows H, isused to supply any required heat to reducer 12 and for the production ofsteam or electric power (at 100).

Referring now to FIG. 8, where like reference numerals indicate likeelements, FIG. 8 illustrates a generalized system that convertsgaseous/liquid carbonaceous fuels. The liquid carbonaceous fuels mayinclude gasoline, oil, petroleum, diesel, jet fuel, ethanol, and thelike; and the gaseous carbonaceous fuels include syngas, methane, carbonmonoxide, hydrogen, gaseous hydrocarbon gases (C1-C6), hydrocarbonvapors, and the like.

In the embodiment illustrated in FIG. 8, gaseous fuel such as syngasfuel or methane is converted, and the system can be divided into tworeactors: a hydrogen generation reactor 80 and a combustor 86. Thehydrogen generation reactor can be further divided into two stages: areducer stage 82 and an oxidizer stage 84. Each stage in the hydrogengeneration reactor can also be considered as a separate reactor.

Preferred designs of the hydrogen generation reactor include a movingbed reactor with one or more stages, a multistage fluidized bed reactor,a step reactor, a rotary kiln, or any suitable reactor or vessel knownto those skilled in the art. In any of the reactor designs, acounter-current flow pattern between solid and gas is used to enhancethe gas and solid conversion. The counter-current flow pattern minimizesthe back-mixing of both solid and gas. Moreover, it improves theconversions of the gas and the solid thermodynamically. The residencetime for solids typically ranges from about 15 minutes to about 4 hours.The reducer residence time typically ranges from about 7.5 minutes toabout 2 hours, and the oxidizer residence time also typically rangesfrom about 7.5 minutes to about 2 hours.

In the reducer 82, gaseous fuel is introduced at or near the bottom ofthe reducer and then moves countercurrently relative to the ceramiccomposite particles. When syngas is used as the fuel, the possiblereactions include:

Fe₂O₃+CO/H₂→2FeO+CO_(2/)H₂O

FeO+CO/H₂→Fe+CO_(2/)H₂O

When natural gas or other methane rich gas is used as fuel, the possiblereactions include:

4Fe₂O₃+CH₄→8FeO+CO₂+2H₂O

4FeO+CH₄→4Fe+CO₂+2H₂O

CH4+H₂O→CO+3H₂

CH4+CO₂→2CO+2H₂

Fe₂O₃+CO/H₂→2FeO+CO_(2/)H₂O

FeO+CO/H₂→Fe+CO_(2/)H₂O

Fuel conversion enhancer such as CO₂, steam, and/or hydrogen can also beintroduced into the reducer stage 82 to enhance methane conversion basedon mechanism similar to that shown in FIG. 3. The heat integrationscheme for methane and other gaseous/liquid carbonaceous fuel conversionis similar to that explained in the solid fuel conversion scheme. FIG.18 illustrates an embodiment for methane conversion.

The solid operating line shown in FIG. 16 is the desirable operatingline for syngas conversion. The operating line for methane and otherfuel conversion shows similar nature as FIG. 16. Although the slope ofthe operating line may change at various operating temperatures, fuelcompositions, and pressures, the stoicheometric ratio between the metaloxide composite particles and the gaseous fuel is usually maintained atfrom about 3:1-1.18:1. As a result, the metal oxide conversion usuallyranges between 33% -85% while greater than 95% of the gaseous fuel isconverted to CO₂ and H₂O. For example, when methane is used, the metaloxide conversion usually ranges between 35% and 70%. When Fe₂O₃ basedceramic composite particles are used, the product from the reducer is amixture of iron and Wuestite.

The gaseous fuel can be pretreated so that it contains less than 750 ppmof H₂S, COS, and some elemental mercury. The reducer configuration andthe ceramic composite particles will allow the H₂S, COS, and mercury toexit the reducer without reacting with the ceramic composite. As aresult, these pollutants can be sequestered along with CO_(2.)

FIG. 9 illustrates the conversion of syngas and iron oxide in a movingbed reducer stage when syngas is used as the gaseous fuel. FIG. 10illustrates the conversion of methane and Fe₂O₃ in a moving bed reducerstage when methane is used as the gaseous fuel. Fe₂O₃-based ceramiccomposite is used in both cases. As can be seen, more than 99.8% fuelconversion can be achieved with ˜50% Fe₂O₃ conversion.

A portion of the reduced ceramic composite is then introduced to theoxidizer 84. In the oxidizer, steam and/or CO₂ is introduced at or nearthe bottom and flows in a countercurrent manner relative to solids. Theoxidizer configuration and gas and solid conversions are similar to thatof the reducer in the solid fuel conversion system discussed previously.

FIG. 11 shows the concentration of the hydrogen product during a movingbed oxidizer operation. Average hydrogen purity of >99% was achieved.

The combustor shown in FIG. 8 is similar to the combustor in the systemfor fuel conversion. A preferred heat integration scheme utilizes theheat from the combustor to provide the heat requirement in the reducer.In a preferred configuration, spent ceramic composite is separated fromthe other particles using a cyclone or other mechanical separationtechniques.

FIG. 12 shows the crushing strength of the ceramic composite. Aftertreatment via reduction-oxidation cycles, the ceramic compositeparticles show a mean compressive strength of about 20 MPa.

FIG. 13 shows the attrition rate of the ceramic composite particles. Theaverage attrition of the ceramic composite particles is <0.6%/reduction-oxidation cycle.

FIG. 14 shows the recyclability of the ceramic composite particles. Theceramic composite particles can sustain more than 100reduction-oxidation cycles without losing their reactivity when syngasis used as the fuel.

FIG. 15 shows the recyclability of the ceramic composite particles. Theceramic composite particles can react with various ranks of coal,syngas, and hydrocarbons for multiple cycles without losing theirreactivity.

When the reducer and the oxidizer are moving beds and the combustor isan entrained bed, the preferred size of the ceramic composite particlesare between about 200 μm to about 40 mm. Such a particle size allows forfluidization in the combustor without fluidizing it in the reducer andthe oxidizer.

Embodiments of the described systems and methods for converting solidfuel and hydrocarbons to carbon free energy carriers can reach an HHVenergy conversion efficiency of up to about 90% for hydrogen productionwith a typical energy conversion efficiency of about 65-80%. Embodimentsof the described systems and methods for converting syngas fuel canreach an HHV energy conversion efficiency of up to about 85% forhydrogen production with a typical energy conversion efficiency of about55-70%. Table 3 shows the performance of a biomass plant for power andH₂ Co-production.

TABLE 3 The performance of a biomass plant for power and H₂Co-production Biomass feed 78800 (lb/hr) HHV input 100 (MW_(th))Hydrogen 3805 (lb/hr) (69.05%) Net Power 4.55 (MW_(e)) (4.55%)Efficiency 73.6 (% HHV)

In one configuration, the reducer can be integrated with a fluidizedcatalytic cracking unit. The reducer converts gaseous hydrocarbons inthe hydrocracker while reducing the ceramic composite. The reducedceramic composite is then introduced to the oxidizer to generatehydrogen. The hydrogen generated can then be used for hydrocracking.

In some cases, catalysts for reactions such as hydrocarbon reforming orwater gas shift can be mixed with the ceramic composite to enhance thefuel conversion. The weight content of the catalyst typically rangesfrom about 0.01% to about 30%.

It will be apparent to those skilled in the art that various changes maybe made without departing from the scope of the invention which is notconsidered limited to the specific embodiments described in thespecification and drawings, but is only limited by the scope of theappended claims.

1.-25. (canceled)
 26. A system for converting fuel comprising: a firstreactor comprising a shell side, a tube side, and a plurality of ceramiccomposite particles, with the ceramic composite particles comprising atleast one metal oxide disposed on a support; a first inlet for providinga fuel to said shell side of said first reactor; and a second inlet forproviding an oxygen-containing gas to said tube side of said firstreactor; wherein the first reactor is configured to reduce the at leastone metal oxide with said fuel to produce a reduced metal or a reducedmetal oxide, and wherein at least a portion of the composite particlesand fuel are directly sent to said tube side of said first reactor wherethe heat of combustion provides heat to the reaction in said shell sideof said first reactor; a second reactor configured to oxidize at least aportion of the reduced metal or reduced metal oxide from the said firstreactor to produce a metal oxide intermediate and a hydrogen rich gasstream; a source of air; and a third reactor communicating with saidsource of air and configured to regenerate the at least one metal oxidefrom the remaining portion of the solids discharged from the said firstreactor and, optionally the solids discharged from the said secondreactor, by oxidizing the metal oxide intermediate. 27.-34. (canceled)35. The system of claim 26, wherein the fuel is a solid fuel selectedfrom the group consisting of coal, biomass, tar, pet coke, tar sands,oil sands, oil shades and combinations thereof.
 36. The system of claim26, wherein at least one of the first reactor and second reactor has afunnel shaped outlet to allow more controlled and homogenous movementsof solids.
 37. The system of claim 26, wherein at least one of the firstreactor, second reactor, and third reactor are connected via anon-mechanical gas sealing and solids control flow devices selected fromthe group consisting of a loop seal, an L-valve, a J-valve, an N-valve,and a zone seal.
 38. The system of claim 26, wherein the first reactorhas an annular opening between the first stage and the second stagewhich allows gas to move from both the solid discharge port of the firststage and the ceiling of the annular opening.
 39. The system of claim26, wherein said second reactor is a moving bed reactor with one or morestages, a multistage moving bed, a rotary kiln, or a step reactorcountercurrent flow between the solids and the gas.
 40. The system ofclaim 26, wherein the second reactor includes a funnel-shaped outlet.41. The system of claim 26, wherein the third reactor is a fastfluidized bed reactor, an entrained bed reactor, a transport bedreactor, or a mechanical conveying system.
 42. The system of claim 26,wherein the third reactor comprises two stages, with the first stagelocated at the bottom being bubbling or turbulent fluidized bed reactorand the second stage being an entrained bed, fast fluidized bed ortransport bed reactor.
 43. The system of claim 26, wherein the thirdreactor is exothermic and at least part of the heat generated in thethird reactor is integrated back to the first reactor to assist thereaction in the first reactor.
 44. The system of claim 26, whereinoxygen is introduced to the first reactor to partially compensate forthe heat required in the first reactor.
 45. The system of claim 26,wherein the first reactor reduces the ceramic composite particles by 20%to 85%.
 46. The system of claim 26, wherein the first reactor convertsthe fuel into an exhaust gas stream that contains at least CO₂ andsteam.
 47. The system of claim 26, wherein the second reactor convertsat least 40% of the gaseous input into product.
 48. The system of claim26, wherein the ceramic composite particles are mixed with a catalyst.49. The system of claim 48, wherein the catalyst is a water gas shiftcatalyst, a steam methane reforming catalyst, or a combination thereof.50. The system of claim 48, wherein the catalyst comprises 0.01% to 30%by weight of the composite particles.
 51. The system of claim 26,wherein sub-stoichiometric amounts of steam and/or CO₂ are introduced tothe second reactor so that more heat is produced in the combustor.